CN1030072A - Carboxylic acid and acid anhydride thereof generate the shortening of alcohol and/or ester - Google Patents
Carboxylic acid and acid anhydride thereof generate the shortening of alcohol and/or ester Download PDFInfo
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- CN1030072A CN1030072A CN88102591A CN88102591A CN1030072A CN 1030072 A CN1030072 A CN 1030072A CN 88102591 A CN88102591 A CN 88102591A CN 88102591 A CN88102591 A CN 88102591A CN 1030072 A CN1030072 A CN 1030072A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
- C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
- C07C29/147—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof
- C07C29/149—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/66—Silver or gold
- B01J23/68—Silver or gold with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/683—Silver or gold with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with chromium, molybdenum or tungsten
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/66—Silver or gold
- B01J23/68—Silver or gold with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/688—Silver or gold with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with manganese, technetium or rhenium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
- B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/8986—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with manganese, technetium or rhenium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
- B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/8993—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with chromium, molybdenum or tungsten
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/17—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrogenation of carbon-to-carbon double or triple bonds
- C07C29/177—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrogenation of carbon-to-carbon double or triple bonds with simultaneous reduction of a carboxy group
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- C07C67/00—Preparation of carboxylic acid esters
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Abstract
A kind of alcohol and/or a kind of carboxylic esters can be by a kind of carboxylic acid or its acid anhydrides by acid or acid anhydrides at high temperature, in the presence of a kind of catalyzer, obtain with H-H reaction, the composition of this catalyzer comprises a kind of alloy, this alloy contains at least one precious metal in (i) periodictable group VIII, (ii) at least one can with group VIII noble metals interfused metal, also comprise an optional carrier, and at least a in the rhenium metal, tungsten, molybdenum.This method is particularly suitable for for example monacid hydrogenation of acetate, and the hydrogenation of toxilic acid or maleic anhydride generation gamma-butyrolactone.
Description
The catalytic hydrogenation of carboxylic acid involved in the present invention and acid anhydride thereof to be producing corresponding alcohol and/or carboxylicesters, and in above-mentioned hydrogenization catalyst for application.
Hydrogenation of carboxylic acids generates corresponding alcohol in the presence of heterogeneous catalyst, in following patent, be known, for example: United States Patent (USP)-A-4524225, United States Patent (USP)-A-4104478, English Patent-A-1534232, English Patent-A-1551741, Deutsches Reichs-Patent-A-3221077 and European patent-A-147219.
United States Patent (USP)-A-4524225 has set forth C
6-C
24Aliphatic acid hydrogenation, this reaction are at 100-300 ℃, 100-300Psig(pound/inch
2) in the presence of zero-valent metal, contact with hydrogen by lipid acid and to carry out, this zero-valent metal is selected from Cu, Cr, and Ru, Pt, Pd, Re and its mixture, and be distributed on the carrier, this carrier can be α, θ or metatitanic acid aluminum oxide, titanium dioxide, AlPO
4Or their mixture.
United States Patent (USP)-A-4104478 has set forth C
4-C
24The production of fatty alcohol, it is at 170-250 ℃, under the 20-140 normal atmosphere corresponding lipid acid is carried out shortening, by a catalyst system, its content is the active rhenium of (a) 1 unit weight and (b) the external metal catalyst that is selected from ruthenium, rhodium, platinum and palladium of 0.25-1.5 unit.
English Patent-A-1534232 has set forth pure preparation, it be with the catalyzer that is loaded with Pd/Re in high-temperature pressurizing, water and/or solvent exist under the situation by the shortening of carboxylic acid, the weight ratio of Pd in this catalyzer: Re is 0.01 to 5: 1.
English Patent-A-1551741 has set forth 1, the single stage method preparation of 4-butyleneglycol, and reaction is carried out hydrogenation of maleic acid in the presence of catalyzer.This catalyzer contains the element in (A) seven races, and ideal has manganese, rhenium or their compound, and (B) element in the 8th family, ideal has ruthenium, rhodium, palladium, osmium, iridium or platinum, and even more ideal is palladium, platinum or their compound or mixture.
Deutsches Reichs-Patent-A-3221079 has set forth the alcoholic acid continuous production, and under high-temperature pressurizing, adopting with the cobalt is that basic catalyzer carries out hydrogenization by acetate.
European patent-A-147219 delivers after request for product requires priority date, in an application that requires than priority date morning, has set forth the hydrogenation of maleic acid with the Pd/C catalyzer.
We are current unsettled European Application Publication No.0198682(BP cabinet No.6347) provide from C
2-C
12Carboxylic acid is produced the method for alcohol and/or carboxylicesters.It is in the presence of the high-temperature pressurizing heterogeneous catalyst carboxylic acid to be contacted with hydrogen, it is characterized in that it can be molybdenum or tungsten that catalyzer contains first kind of composition, and second kind of composition is a kind of precious metal in the VIII family in the periodic table of elements.
At last, we are current unsettled European Application Publication 0198681(BP cabinet No.5930) revealed the production method that from acetate, obtains ethanol or from propionic acid, obtain propyl alcohol, this method be included in high temperature and pressure in the 1-150bar barometric pressure range in the presence of catalyzer, the acetate of gas phase or propionic acid are contacted with hydrogen.The main component of this catalyzer is a kind of precious metal and (II) rhodium in (I) periodic table of elements VIII family.
In above-mentioned reaction owing to the problem that adopts heterogeneous hydrogenation catalyst to bring is to have produced unwanted alkane, for example methane and ethane, this side reaction has reduced the selectivity of desired product.
We have found to adopt alloy catalyst can reduce alkane and have formed this problem at present.
So on the one hand, the invention provides the production method of producing correspondent alcohol or carboxylicesters with the carboxylic acid or anhydride, this method is included in high temperature and makes carboxylic acid or anhydride and H-H reaction in the presence of the composition catalyzer.The composition of said composition catalyzer contains alloy and (II) at least a metal that can constitute alloy with the precious metal fusion of VIII family of at least a precious metal in a kind of (I) periodic table of elements VIII family.
Hydrogen can obtain in a large number, can want or further not purify, and the purification that needs can be to remove carbon monoxide.
Method of the present invention is applicable to carboxylic acid and carboxylic acid anhydride.Carboxylic acid or carboxylic acid anhydride can be saturated or unsaturated, and the derivative of monobasic, binary or polyprotonic acid and its acid anhydride all may be utilized.Suitable carboxylic acid or anhydride can contain 2-12 carbon atom.
Suitable monoprotic acid comprises that molecular formula is the acids of R-COOH, and wherein R can be aliphatics, aromatics or the araliphatic base that replaces or do not replace.This acid is hydrogenated and generates molecular formula is RCH
2The alcohols of OH.Suitable R base Ke Yun Rice-seedlings
2-C
12Alkyl.For example suitable monobasic acid comprises acetate, propionic acid, butyric acid and enanthic acid, and comparatively the ideal monobasic acid is an acetate.
About the composition of catalyzer, the precious metal of periodic table of elements VIII family is palladium, platinum, rhodium, ruthenium, osmium and iridium, and wherein palladium, rhodium, ruthenium are even more ideal.Can silver, gold, copper, nickel, rhodium, tin, cobalt, aluminium, manganese, gallium, iron, chromium and platinum be arranged with the metal that palladium forms alloy, wherein silver, gold, platinum, wherein silver, gold, copper are even more ideal, and best is silver.Can iron, cobalt, manganese, germanium, rhenium be arranged with the metal that ruthenium forms alloy.
Though the alloy of a kind of catalyst composition contains a kind of (I) and (II), wherein (I) is a kind of precious metal of VIII family in the periodic table of elements at least, (II) is at least a metal (after this being called component (A)) that can fuse into alloy with the precious metal of above-mentioned VIII family, this catalyzer is used as catalyzer in the hydrogenation of a divalent carboxylic acid, incorporate one or more kind components in the catalyzer into but be preferably in.
(as component (B)) a kind of metal in rhenium metal, tungsten or the molybdenum is at least incorporated in suggestion into.
A carrier (as component (C)) is incorporated in suggestion into, and the carrier that is fit to comprises high surface area graphitized carbon (HSAG), graphite, activated carbon, silicon-dioxide, aluminum oxide and silica/alumina, wherein with HSAG carbon and high surface area silica for well.
Particularly suitable carrier is high surface area graphitized carbon (explanation is arranged in GB-A-2136704), and it can be powder and pill shape, and ideal carbon should be Powdered, and its size depends on reactor used type.
Carbon is porous carbon, BET method one surface-area of carbon, the long-pending feature that has determined carbon of baseplane and edge surface.The BET-surface-area is by the adsorption of nitrogen decision, employing be Brunauer Emmett and the Teller J.Am. chemical industry bo.309(1938 of association) method.
The baseplane is long-pending to be to be determined by the heat of adsorption of (carbon) alkane absorption normal heptane just-32.Its method is described in the journal A314 475-498 of the Royal Society page or leaf, especially is worth with reference to 489 pages.Edge surface is long-pending to be to determine that by the heat of adsorption of the carbon absorption normal heptane of propyl carbinol the technology that its method was mentioned above disclosing especially can be with reference to 495 pages on the Royal Society's journal.
The carbon that uses among the present invention, its BET-specific surface area is at least 100m
2/ g, 200m
2/ g is better, it would be desirable 300m
2/ g.The BET-specific surface area preferably is not more than 1000m
2/ g is especially to be no more than 750m
2/ g is best.
Comparatively ideal BET-specific surface area should be not more than 4: 1 with the ratio of baseplane surface-area, preferably is not more than 2.5: 1, and optimum regime is 1.5: 1.
Comparatively ideal baseplane surface-area should be 10: 1, best 50: 1 at least with the ratio that edge surface amasss.Although be no more than 200: 1 usually in practice, we do not think that it has upper-limit ratio.
Comparatively the ideal carbon support can prepare through Overheating Treatment with carbonaceous starting material.This starting material can be oleophylic graphites, as English Patent 1,168, reveal in 785, also can be carbon black.
Yet the carbon that oleophylic graphite contains is superfine sheet particulate, is not the suitable material of doing support of the catalyst, should avoid using it as far as possible, and similarly consideration also is applicable to carbon black, because it also has very tiny particle.
Desirable material is from vegetable material deutero-activated carbon, as coconut carbon or from mud coal, coal or from the polymkeric substance of carbonization.These materials form the ideal particle through Overheating Treatment, and its size is not less than the requirement of the ideal carbon support of above-mentioned requirements.
The ideal starting material have following properties: BET-specific surface area at least 100, even more ideal is 500m at least
2/ g.
Preparation carbon support comparatively ideal heat treatment step has clear and definite feature: (1) heats carbon in rare gas element, temperature is from 900 ℃ to 3300 ℃, (2) temperature of oxidation of coal is from 300 ℃ to 1200 ℃, and heat in rare gas element (3), and temperature is from 900 ℃ to 3000 ℃.
When oxygen (for example being air) during as the oxidation mediators thing, oxidation step ideal temperature is between 300 ℃ to 600 ℃.
The time length that heats in rare gas element is not crucial, and heating carbon will be enough to make carbon that desired variation takes place to the required time of desired top temperature.
Very natural, when carbon fully burnt, oxidising process was not necessarily leaveed no choice but carry out.Gaseous oxidation vehicle is adopted in suggestion, gives by certain control ratio, to avoid peroxide.The vectorial example of gaseous oxygen has steam, carbonic acid gas and some to contain the gas of molecular oxygen, as air.Comparatively the ideal oxidation is that weight with carbon in the oxidising process is benchmark, and it is 10%, 15% better that weight loss is at least.
The weight loss of carbon preferably is no more than 40% in the oxidising process, be no more than carbon weight 25% for better.
The speed that the oxidation mediators thing provides is preferably in the required weight loss of appearance after at least 2 hours, and even more ideal situation is at least 4 hours.
Can use nitrogen or certain rare gas element at the needs rare gas element.
The ideal silicon carrier has high surface area, typically is greater than 50m
2/ g.
The catalyst component that is fit to comprises, the weight from 0.1 to 20% of component (A), and ideal weight is from 1 to 10%, and the weight of component (B) is from 0.1～20%, and ideal situation is from 1～10%, and remaining catalyzer comprises carrier.
A kind of metal or the multiple metal further modification of the composition of catalyzer by incorporating I A family or II A family into.
The alloy that constitutes the component (A) that catalyzer of the present invention forms is with various appropriate means productions, for example use the method or the colloidal method of heat, composition (A) also can mix with composition (B) then, composition (A) and (B) can by traditional method independent or combination be applied to carrier.
Above-mentioned carried catalyst is formed and can be produced by a kind of method, this method comprises that (I) deposits at least a precious metal chemical complex on carrier, and at least a compound that can form a kind of a kind of metal of alloy with VIII family precious metal, said compound can decompose/be reduced into metal with the method for heat, the composition that (II) obtains in step (I) in heating under certain temperature and the condition, make compound thermolysis/be reduced into metal, and form its alloy, a kind of compound of deposition on the composition that (III) obtains in step (II), this compound has rhenium at least, a kind of metal in these metals of tungsten or molybdenum.
Being used to produce the step that the Perfected process of above-mentioned supported catalyst composition comprises is:
(I) is with a kind of solution or solution (ⅰ) and (ⅱ) impregnated carrier, at least a solubilized VIII of solution (ⅰ) family precious metal chemical complex, but this compound pyrolysis/be reduced into precious metal, solution (ⅱ) soluble compound, but this compound thermolysis/be reduced into metal, this metal is a kind ofly can form alloyed metal with VIII family precious metal at least, removes solution then.
(II) under certain condition and temperature, the composition that heating obtains in step (I) makes compound can decompose/be reduced into metal, forms its alloy simultaneously.
(III) is soaked in the composition that obtains in the step (II) with a kind of compound, and this compound has a kind of metal in rhenium, tungsten or the molybdenum at least, removes this solvent then.
Used solvent can be identical in present method step (I) and the step (III), also can be different, preferably identical, and can also be with any suitable solvent, for example water.
Soak into carrier technique with metal compound solution, and then remove that to desolvate be known in the prior art, need not to remake detailed descriptionthe, this technology comprises the humidity technology and the excess solution technology of beginning.
In step (II), composition is suitable under the temperature more than 600 ℃ heating and reaches thermolysis/reduction, and heating/reductive metallic compound becomes metal element and generates its alloy.This heating steps is suitable for finishing in the presence of rare gas element, as nitrogen.Though about 600 ℃ is the temperature of indication, palladium and silver are subjected to the thermosetting alloy under this temperature, and optimum temps also depends on the special combined characteristic of institute's containing metal.
Best, between step (I) and step (II), to insert a further step, and can select step (III) thereafter arbitrarily, the carrier drying that will soak in this step, the temperature of heating are adapted in the 50-150 ℃ of scope.By the technician who is familiar with prior art this step being incorporated in the step (II), will be useful.
Then, be step (IV) after the step (III), but in this step pyrolytic/reducible rhenium, the compound of at least a metal in tungsten or the molybdenum is by pyrolysis/be reduced into metal form.In other words, this also can finish in the catalyst activation step.
Molybdenum, tungsten or the rhenium compound (can decompose/be reduced into metal or oxide compound) that are fit to comprise that metal-salt and multiple salt, metal wherein are to be present in the anionic part, for example ammonium molybdate or ammonium tungstate.
The precious metal chemical complex (can decompose/be reduced into precious metal) that is fit to comprising: as precious metal salt, as carboxylate, halogenide, nitrate, contain the ammonium salt of precious metal in the anionicsite, for example tetrachloro palladium ammonium.The metallic compound metal-salt with the ability that fuses with precious metal that is fit to is as nitrate, carboxylate salt and halogenide.
Periodic table of elements I A family, whenever the metal of II A family or IV A family can joining in the catalyst composition that its prepares, and the alloy composite of carrier soaks with regard to available a kind of soluble metal compound solution like this.In other words, solvable more fish hawk boat rank Kun China fir gathers around that to water cane onion brown little
Comparatively the ideal catalyzer comprises (ⅰ) a kind of palladium/silver alloys, (ⅱ) rhenium is stated from the carrier of the high surface area graphitized carbon of talking about among English Patent-A-2136704.
Before carrying out production stage of the present invention, preferably allow catalyzer under hot conditions with hydrogen or hydrogen/rare gas element, for example nitrogen mixture contact activates, the time that is fit to is 1-20 hour.Temperature is adapted in the 200-350 ℃ of scope, and in other words, catalyzer can activate by being heated to temperature of reaction when reagent exists.
When adopting monobasic acid, method of the present invention is suitable for operating in temperature is 100-300 ℃ of scope, and preferably from 150 to 250 ℃, pressure is lower than 50 crust.
Present method can be carried out under liquid phase or gas phase condition.
Present method can be interrupted, also can carry out continuously, preferably successive.Catalyzer can adopt fixed bed, and the form of moving-bed or fluidized-bed, gas space-time speed per hour are suitable for when 50-50000 per hour
-1In the scope, preferably from 2,000 to 30,000 o'clock
-1
Remove in the external production process of the present invention of alcohol and also produce corresponding byproduct ester usually, for example the hydrogenization of acetate produces ethyl acetate usually, and the hydrogenization of propionic acid produces propyl propionate usually.The ratio of the ester that generates depends on the characteristic of catalyzer.If desired, the content of ester can also further increase, and can add extra carboxylic acid and a kind of effect of acid is incorporated in the catalyzer to promote esterification on the spot.Thereby might produce a kind of product and mainly contain carboxylicesters.Particularly operation in the low conversion of liquid phase for example is less than 50%.
The selectivity that an advantage of production process of the present invention is the monobasic acid hydrogenization can increase needed product (alcohol/ester) by consuming unwanted product (alkane).
Method of the present invention can be used for the hydrogenization of di-carboxylic acid and acid anhydride thereof, especially the hydrogenization of unsaturated dicarboxylic acid and acid anhydride thereof.The di-carboxylic acid that is fit to and pentanedioic acid, glutaric anhydride, hexanodioic acid, own dianhydride, Succinic Acid, succinic anhydride, toxilic acid and the maleic anhydride of acid anhydride thereof.
The hydrogenization of toxilic acid or maleic anhydride produces that the r-butyrolactone is normally difficult to be finished because the r-butyrolactone can with hydrogen further reaction produce 1,4 butyleneglycol and tetrahydrofuran (THF).Except reducing undesirable alkane, the alloy catalyst among the present invention can also further stop the reaction of r-butyrolactone to produce byproduct, and for example 1,4-butyleneglycol and tetrahydrofuran (THF).
Thereby on the other hand, the invention provides and a kind ofly produce the method for r-butyrolactone from toxilic acid or maleic anhydride, the catalyzer that this kind method is included in aforementioned component (A) exists makes heating of toxilic acid or maleic anhydride and hydrogen react down.
Ideal component (A) comprising: or palladium or ruthenium or rhodium, better situation palladium is as precious metal (I) or silver, gold or copper, and even more ideal is that silver has the metal that becomes the ability of alloy with palladium as (ⅱ).Special ideal alloy is the alloy of palladium and silver.Component (A) can be as catalyzer or with or without the component that has the front to talk about (B) and (C), although component (C) is a very ideal carrier.The ideal carrier is exactly the HSAG carbon of talking about previously.
Catalyzer is used for preferably being activated before the production process, and its method as previously mentioned.
Production process can be alternate, also can be that successive and Malaysia acid or anhydride can be introduced into or liquid phase or vapour phase.In liquid phase, should adopt solvent to maleic anhydride, solvent can or water or inert organic solvents, for example 1,4-diox, water are suitable for doing the solvent of toxilic acid, 1, the 4-diox is suitable for doing the maleic anhydride solvent.
About the condition of reaction, suitable temperature range is 50-350 ℃, and ideal situation is 150-300 ℃, and pressure is in the 1-300bar scope, and ideal situation is 10-150bar.The suitable scope of liquid space-time speed (LHSV) of operate continuously is 0.05-10, and ideal situation is 0.1-5.In liquid-phase operation, suitable gas is 1: 300 with the ratio scope of liquid, and ideal situation is 1: 100.
Last a kind of situation provided by the invention is that catalyst component is suitable for being used in the hydrogenization of carboxylic acid and acid anhydride thereof, and its composition comprises the component (A) talked about previously and (C).
Catalyst component is suitable for incorporating into the component of talking about previously (B).
Particularly the ideal catalyst component is palladium and the alloy of silver and the HSAG carbon of talking about previously, also can incorporate rhenium arbitrarily into.
The present invention now will be further described with reference to following example and comparative experiments.
The graphited carbon of project in following example and comparative experiments " HSAG carbon " expression high surface area, its preparation is as follows with characteristics:
Carbon as carrier is that the activated carbon ACL40 that indicates that CeCa company betrays is prepared into carrier.Activated carbon is done following thermal treatment.Allow carbon in nitrogen, be heated to 1700-1800 ℃, about one hour, when 1700-1800 ℃ of temperature, kept 20 minutes, then with the carbon cool to room temperature from room temperature.The water of cooling heat exchanger is used for lowering the temperature about one hour, in the kiln of a rotation, carbon is heated to 520 ℃ then, the required time can be 5% o'clock weight loss according to rate of weight loss hourly, and 20% this experience is determined, the nitrogen of then carbon being put into temperature and be 1700-1800 ℃ heats, and in nitrogen cool to room temperature, the graphitiferous carbon that will produce then grinds into the 16-30 order, according to U.S.'s industrial technology standard specifications.
Treated carbon has following characteristic:
BET-specific surface area 628m
2/ g
Baseplane surface-area 460m
2/ g
Edge surface amasss 8m
2/ g
The ratio 1.36 of BET-ratio/baseplane surface-area
The ratio 58 that baseplane/edge surface is long-pending
Then with carbon in containing 5% aqueous hydrochloric acid backflow 2-3 hour, filter and use distilled water flushing, in distilled water backflow 2-3 hour, a filtration and a dry night in 100 ℃ vacuum oven.
Preparation of catalysts-based on the catalyzer of palladium
The nominal carrying capacity is to determine according to the weight that is added to the metal of carrier in following step, recently represents with the percentage of vehicle weight.
Example 1
To contain soluble Palladous nitrate and silver nitrate aqueous solution and be added in the HSAG carbon, water removes in the vaporizer of a rotation and anhydrates, and will put into 100 ℃ vacuum oven dried overnight through the carbon that soaks into then.Select the content of various compositions, the carrying capacity that the composition that gets provides is as follows: 1.7% silver medal, and 2.5% palladium then with composition cools, is transformed in the Glass tubing, heats in nitrogen again, and condition is as follows:
-being heated to 600 ℃ by room temperature, the time is 8 hours, under 600 ℃ of temperature, kept 8 hours, cool to room temperature in nitrogen then, the catalyst composition that is produced is designated as catalyst A.
Example 2
Allow the aqueous solution of catalyst A and rhenium heptoxide then, solvent is removed in the vaporizer of rotation, and with composition dried overnight in 100 ℃ vacuum oven, the catalyzer of the carrying capacity that provides-1.7% silver medal, 2.5% palladium, 5% rhenium, the catalyzer that is produced is designated as catalyst B.
Comparative experiments 1
Except nitrate is removed, repeat the step of example 1 from preparation.Select the content of heterogeneity, the carrying capacity that provides composition is as follows :-2.5% palladium.Second difference is exactly that its composition heats in nitrogen under the following conditions:
-being heated to 300 ℃ from room temperature, the time need surpass 6 hours, keeps 10 hours at 300 ℃ then, then is cooled to room temperature in nitrogen.
The catalyst composition that is produced, said composition are not according to of the present invention, are designated as catalyzer C.
Comparative experiments 2
Repeat the step of example 2, replace catalyst A, provide the carrying capacity of composition :-2.5% palladium, 5% rhenium with the catalyzer C in the comparative experiments 1.
The catalyst composition that is produced is designated as catalyzer D not according to the present invention.
Comparative experiments 2A
Except the temperature of composition heating with 300 ℃ of 600 ℃ of replacements, repeated experiments 1.Then compare the step of experiment 2, catalyzer is designated as catalyzer D1.
Example 3-6
With producing the Ag/Pd/Re/HSAG catalyzer with example 1 and 2 similar steps, the scope of silver-colored carrying capacity is as follows :-
Example 3, catalyzer E-0.8%Ag/2.5%Pd/5%Re/HSAG
Example 4, catalyzer F-3.3%Ag/2.5%Pd/5%Re/HSAG
Different Pd carrying capacity is as follows :-
Example 5, catalyzer G-1.7%Ag/1.25%Pd/10%Re/HSAG
Example 6, catalyzer H-1.7%Ag/1.25%Pd/10%Re/HSAG
The detailed preparation process and the composition of catalyzer are listed in the table 1.
Example 7-9
Use and example 1 and 2 similar steps, to produce following Cu/Pd/Re/HSAG the Silver Nitrate except replacing with cupric nitrate
Catalyzer :-
Example 7, catalyst I-0.6%Cu/2.5%Pd/5%Re/HSAG
Example 8, catalyzer J-1.0%Cu/2.5%Pd/5%Re/HSAG
Example 9, catalyzer K-0.5%Cu/1.25%Pd/10%Re/HSAG
Detailed preparation process and catalyst composition are listed in the table 1.
Example 10
With with example 1 and 2 similar steps, except replacing Silver Nitrate, produce catalyzer (L) with gold trichloride, its composition is :-1.7%Au/2.5%Pd/5%Re/HSAG
Detailed preparation process and composition are listed in the table 1.
Example 11
Use and example 1 and 2 similar steps the Silver Nitrate except replacing with nickelous nitrate, to produce catalyzer (M), its composition is :-0.5%Ni/2.5%Pd/5%Re/HSAG
The detailed preparation process and the composition of catalyzer are listed in the table 1.
Comparative experiments 3
Except relevant ratio has been done to revise, repeat the step of comparative experiments 2, produce catalyzer (N), its composition is :-1.25%Pd/10%Re/HSAG
The detailed preparation process and the composition of catalyzer are listed in the table 1.
Characteristics with the X-ray diffraction alloy catalyst
Before rhenium soaked into the stoichiometry and average lattice dimensions of determining them, alloy was checked by X-ray diffraction (XRD).
Alloy and composition thereof are the face-centered cubic architecture, and alloy has lattice parameter between their parent element.Accurately measure the lattice parameter of alloy with internal standard, available interpolation technique is estimated its composition, supposes between composition and lattice parameter to exist linear relationship.And some phases can not be measured lattice parameter with enough accurate methods in some catalyzer, carry out the composition analysis.The average crystalline size of alloy is observed in certain limit concerning the catalyzer that only contains palladium, and its data are measured with XRD together with the composition of catalyzer, are listed in the table 2.
Palladium/silver
Most palladium and silver are merged into a kind of alloy, and except only forming a kind of alloy in the external all example of example.From the XRD(X ray diffraction) the composition information that obtains is very consistent with the composition of surveying with XRD to a certain extent.
Palladium/copper
Some copper is invisible to X-ray diffraction (XRD), the people is associated exist as high dispersive and unbodied situation.Remaining copper is merged into palladium/copper alloy, also contains suitable metallic palladium content in exemplar.
Palladium/gold
This exemplar comprises a kind of mixture that has added the alloy composite of metallic palladium.Suggestion more is being necessary to develop better alloy and catalyzer as well as possible under the specific conditions.
Palladium/nickel
Seemingly need longer heat-up time or higher temperature, so that better impel latitude to support palldium alloy.
Palladium/rhenium
Its catalyzer is similar to the composition of catalyzer D, and the preparation method is also similar, and unique difference is that HSAG thermal treatment is different and slightly different performance when analyzing with xrd method.This catalyzer only contains a kind of crystalline palladium phase metal, and the size of its average crystalline is greater than 100 dusts.
Catalyst experiment
(1) hydrogenization of acetate
Normal atmosphere is in the 1-11bar scope during experiment, in the catalyzer of the 2.5mls corrosion-resistant stainless steel pipe that to add an internal diameter be 6-7mm, reactor tube is contained in the tube furnace, make catalyzer heat-activated in hydrogen then, temperature or be 280 ℃, or be 300 ℃, 2 hours time, in said temperature, continue 1 hour then.After the activation catalyzer is cooled to the temperature of required reaction in hydrogen.Again the mixture of carboxylic acid gas and hydrogen is passed through catalyzer, normal atmosphere is adjusted on the value that needs with a back pressure regulator, gas/hydrogen mixture then forms in a gasification zone.Will separately measure acetic acid solution and hydrogen, leave the product of reactor, vapour and gas are taken a sample on pipeline, and analyze with solution-air chromatography (gLC).
Temperature is inserted in the beds by a thermocouple and is measured.
Typical product mixture contains certain pure and mild ester (latter is formed by alcohol and unreacted acid esters), also has a certain amount of dialkyl ether trace, and aldehyde and byproduct methane, ethane, (only containing propionic acid) propane.In general its main products of the catalyzer of carbon silicon carrier is alcohol, particularly passes through height conversion.
Purpose, conversion and selectivity to above-mentioned example have been done calculating respectively.The carboxylic acid ratio of hydrogenation does not change into alkane, and thus, its selective meter understands that catalyzer does not have the alkanisation ability when finishing hydrogenization.In all examples (unless otherwise indicated outside) have only very in a small amount that the dialkyl ether and the aldehyde of (＜2%) form.
Definition:
WHSV=weight hourly space velocity=kilogram liquid feeding/kilogram catalyzer/per hour
LHSV=liquid hourly space velocity degree=liter liquid feeding/liter catalyzer/per hour
The acid of the alkyl that is produced=kilogram converts all products to, except the per kilogram catalyzer every
Hour the alkane byproduct outside.
Example 12-15
Acetate carries out hydrogenation through the catalyst composition B of example 2, and WHSV is about 3.8, (LHSV=1.34h
-1), hydrogen is about 10: 1 mol to the ratio of acetate, and pressure is 10.3bar.The activation temperature of catalyzer is 280 ℃ in all cases.Its collection and is plotted among Fig. 1 in table 3.
Turn round and do not observe deactivation phenomenom in 24 hours.
Comparative experiments 4-7
Repeat the step of example 2-5 except replacing the catalyst composition B with catalyst composition D.
Collection is in table 3 and see Fig. 1.
Its result shows that the palladium and the alloy of silver have improved selectivity, make the alkyl that is produced slightly descend simultaneously.
Comprised D for comparison purposes, it is not according to the present invention.The advantage that obtains by the alloy of palladium and silver as we can see from the figure.Can obtain identical throughput (P by having higher optionally B component by means of the temperature that is fit to
1) (S
1Greater than S
2).Same higher throughput also can be at constant selectivity (S
2) use B component to obtain (P
2＞P
1).
Example 16-19
Except replace the catalyst B in the enforcement 2 with the catalyzer E in the example 3, repeat the process of example 12-15.
The result is illustrated in the table 4.
Example 20-23
Except replace the catalyst B in the example 2 with the catalyzer F in the example 4, repeat the process of example 12-15.
Its result is illustrated in the table 4.
Comparative experiments 8-11
Except using the catalyzer D among the comparative experiments 2A
1Replace repeating the process of example 12-25 outside the catalyst B in the example 2.
Its result is illustrated in the table 4.
Table 4
Palladium/silver/rhenium/HSAG
The result who is provided in the table 4 is illustrated among Fig. 2 with the form of chart.The silver of Jia Ruing forms palladium/rhenium/HSAG catalyzer as alloy and palladium and changes productivity and pilot wire optionally as seen from Figure 2.By a kind of the carrying out in the available two kinds of methods of the improvement of selecting suitable service temperature catalyst performance.When throughput was 1Kg/Kg catalyzer/h, selectivity of catalyst was owing to adopt and contain silver alloys and can bring up to 94% from 92%.In other words, be 92% o'clock in selectivity, its throughput can be brought up to 1.6Kg/Kg catalyzer/h from 1.0.More dispersing arranged on the pilot wire in general, thereby at high temperature can from alloy, obtain more benefit, promptly high throughput and low selectivity.
Example 24-27
Except replace the catalyst B in the example 2 with the catalyst I in the example 7, repeat the step of example 12-15.
Its result is illustrated in the table 5.
Example 28-31
Except the catalyzer J with example 8 replaces repeating the step of example 12-15 example 2 catalyst B.
The results are shown in Table 5.
Example 32-35
Except the catalyzer L with example 10 replaces repeating the step of example 12-15 example 2 catalyst B.
The results are shown in Table 5.
Example 36-39
Except replace the catalyst B in the example 2 with the catalyzer M in the example 11, repeat the step of example 12-15.
The results are shown in Table 5.
Table 5
Palladium/copper (gold or nickel)/rhenium/HSAG
The result who is provided in the table 5 is illustrated among Fig. 3 with the form of chart, the selectivity ratios silver that this shows copper is greatly improved, the selectivity of methane has reduced 55% at least, and the selectivity of ethane has reduced 15%, but following productivity also has bigger reduction.This shows that copper alloy compares with silver alloys that generally speaking benefit is less.
Selectivity can bring up to 93% from 95% when productivity was 1.0Kg/Kg catalyzer/h as seen from Figure 3.
Gold utensil has the activity identical with silver.
The selectivity of nickelalloy has increased.
Example 40-43
Except replace the catalyst B in the example 2 with the catalyzer G in the example 5, repeat the step of example 12-15.
Its result is illustrated in the table 6.
Example 44-47
Except replace the catalyst B in the example 2 with the catalyzer H in the example 6, repeat the step of example 12-15.
Its result is illustrated in the table 6.
Example 48-51
Except with the catalyst B in the catalyzer K replacement example 2 of example 9, repeat the step of example 12-15.
Comparative experiments 12-15
Except with the catalyst B in the catalyst n replacement example 2 of comparative experiments part, repeat the step of example 12-15.
Its result is illustrated in the table 6.
Table 6
(2) hydrogenization of toxilic acid and maleic anhydride
Preparation of Catalyst
Below nominal carrying capacity be defined as the weight (not being salt) that joins the metal on the carrier and recently represent with the percentage of vehicle weight.
Comparative experiments 16-catalyst P
The aqueous solution that contains soluble Palladous nitrate is joined HSAG, remove in the vaporizer of a rotation and anhydrate, saturant carbon is a dry night under 150 ℃ temperature.Selecting the nominal carrying capacity of Palladous nitrate is 30% palladium, with the catalyzer cooling, transfers in the Glass tubing, and heats in nitrogen gas stream under the following conditions then; Be heated to 300 ℃ from room temperature, 8 hours temperature rise time, kept 8 hours down at 300 ℃, in nitrogen, be cooled to room temperature again.
With this composition and rhenium heptoxide aqueous solution, more this solvent is put into the vaporizer of a rotation and removed then.150 ℃ one night of stove inner drying, obtain the catalyzer of nominal carrying capacity for-3% palladium and-3% rhenium.
Example 52-catalyzer Q
Except Silver Nitrate is joined the palladium nitrate solution, repeat the step of comparative experiments 16, select various composition total amounts and just obtain nominal: 1.54% silver medal as download, 3% palladium, 3% rhenium, second difference is that its composition is before adding rhenium, use following condition, composition is heated in nitrogen gas stream.Be heated to 600 ℃ from room temperature, the heating-up time is 8 hours, keeps 8 hours down at 600 ℃ then, cool to room temperature in nitrogen again.
Example 53-catalyzer R
Repeat the step of example 52, obtain a composition, nominal carrying capacity: 3% palladium, 3.07% silver medal, 3% rhenium.
Example 54-catalyst S
Repeat the step of example 52, draw a composition, nominal carrying capacity: 3% palladium, 6.14% silver medal, 3% rhenium.
Catalyst experiment
(1) general rhythmic reaction method
Comparative experiments 17 and 18 and example 55-60.
Clean one 30 milliliters stainless steel autoclave, pack into then catalyzer (being generally 1.0g) and an amount of solution with nitrogen.For the hydrogenation of acid anhydride, this solution is that the maleic anhydride by 20g is dissolved in 120g1, forms in the 4-diox.For the hydrogenation of toxilic acid, this solution is to be added in the deionized water of 120g by the maleic anhydride of 20g.Clean autoclave with hydrogen then, be pressurized to 80barg(5 ℃/min with hydrogen again, 1000rpm), heating and stirring reach till 230 ℃ up to temperature, kept under this temperature 12 hours and stir continuously, stopping after finishing in this cycle allows the autoclave cool to room temperature.The solution-air chromatography is adopted in gaseous state and liquid sampling and analysis, and its result is illustrated in table 7, the table 8.
(2) research continuously
Comparative experiments 19 and example 61
A 0.1dm is adopted in the continuous experiment of hydrogenation of maleic acid catalyzer (maleic anhydride that contains 13% gold medal in deionized water)
3The pilot scale technique device.Experiment is under 725psig, and it is in the stainless steel reactor of 25mm that the 100mls catalyzer adds internal diameter, and this reactor can be three zone heating (top, catalyst bed, bottom) that separate.Catalyzer is 50: 50 at 500Psig, at the ratio of air-flow hydrogen and nitrogen, is heated to 280 ℃, and temperature rise rate per hour is among 15 ℃ the slow Hui of condition high post net for catching birds or fish hour.After the activation, catalyzer is cooled to desired temperature of reaction in hydrogen.Allow the mixture of toxilic acid liquid and hydrogen pass through catalyzer then, pressure is adjusted to the value of requirement by an air-operated automatic pressure control valve.
The performance of catalyzer is to assess at 10 hours prerun and 10 hours material balance, to obtain the situation of stable state.Product steam, gas and liquid sampling.Gas/liquid is separated and is analyzed employing line solution-air chromatography, and the measurement of temperature is top, middle layer and the bottom of a thermocouple being inserted catalyst bed.
Its result is illustrated in the table 9.
Table 9
Catalyzer 3%Pd-0.3%Re/HSAG 3%Pd-3%Ag-3%HSAG
（P） （R）
Example CT-19 61
Temperature ℃ 200-260
*250-260
*
Throughput (Kg/Kg catalyzer/h) 0.34 0.33
Product
Selectivity %
Methane 11 0
（BuoH+ProH）
Butanols+propyl alcohol
THF 2 6
r-BLO 36 89
BDO 5 1
Succsinic acid-2
Condition: LHSV=1, GHSV=2000, P=725 pound/square English inch
H
2: toxilic acid=60: 1
*Because the range of temperature that reaction produces
Abbreviation: THF-tetrahydrofuran (THF)
-rBLo-r-butyrolactone
-BDo-1, the 4-butyleneglycol
The contrast experiment 20
Repeat the hydrogenation step of the maleic anhydride of example 55 to 60, except be attached to the catalyzer of aluminum oxide the preparation method of the intermediate 3%Pd/HSAG of comparative experiments 16 with 3%Pd.
The result is illustrated in the table 10.
Example 62
Repeat comparative experiments 20, except with catalyzer 3%Pd/6%Ag Al
2O
3Replace 3%Pd/Al
2O
3Outward, the former is (an omission rhenium) with the same method preparation of the catalyzer Q in the example 52.
The result is illustrated in the table 10.
Example 63
Repeat comparative experiments 20, except with catalyzer 3%Pd/6%Ag/3%Re/Al
2O
3Replace 3%Pd/Al
2O
3Outward, the former uses the method for catalyzer Q in the example 52 to prepare.
The result is illustrated in the table 10.
Comparative experiments 21
Except that 3%Pd is attached to the catalyzer of aluminum oxide, repeat the step of toxilic acid oxidation in the example 55 to 60.This aluminum oxide prepares with the same method of the 3%Pd/HSAG intermediate of preparation comparative experiments 16.
The result is shown in the table 11.
Example 64
Except with 3%Pd/6%Ag/Al
2O
3Catalyzer replace 3%Pd/Al
2O
3Outside the catalyzer, repeat comparative experiments 21, the former is (an omission rhenium) with the same method preparation of the catalyzer Q in the preparation example 52.
The result is illustrated in the table 11.
Example 65
Except with 3%Pd/6%Ag/3%Re/Al
2O
3Catalyzer replaces 3%Pd/Al
2O
3Outside the catalyzer, repeat comparative experiments 21, the former is with the method preparation of catalyzer R in the example 53.
The result is illustrated in the table 11.
Table 11
Preparation of catalysts-ruthenium-based catalyst
Comparative experiments 22-catalyzer T
High surface area graphitized carbon (5g) is soaked in the Ru(No of distilled water diluting to 50ml) (No
3) solution (7.3 weight %Ru) (1.61g) in, this solution is in 70 ℃ and-800 millibars of (mbar) pressure rotation evaporation drying down, sample in 120 ℃ of vacuum ovens dry 16 hours, then under mobile 1 atmospheric pressure hydrogen air-flow 300 ℃ reduced 4 hours.Air-flow converts nitrogen to, and catalyzer cools off under this gas.Be soaked in by the graphite of rutheniumization and contain Re
2O
7In the aqueous solution (0.65g) (50ml), 70 ℃ and-800mbar pressure under Rotary drying, then in vacuum oven in 120 ℃ dry 16 hours down.
Nominal catalyst loading:
2.35 weight %Ru-5 weight %Re/ high surface area graphitized carbon.
Example 66-catalyzer U
The high surface area graphitized carbon is soaked in the Ru(No of distilled water (100ml)) (CO
3)
3Solution (7.3 weight %Ru) (1.61g) and Fe(No
3)
39H
2O(0.47g) in.With this solution rotating evaporation drying, and dry in vacuum oven, with catalyzer T method.Equally reduce with catalyzer T then, but, convert air-flow to nitrogen, specimen temperature rises to 800 ℃.Sample cools off under nitrogen gas stream.Re
2O
7With being soaked in the sample as the same method of catalyzer T.
Nominal catalyst loading:
2.35 weight %Ru-1.3 weight %Fe-5 weight %Re/ high surface area graphitized carbon.
Example 67-catalyst V
Except with CO(NO
3)
26H
2O(0.30g) replace Fe(NO
3)
39H
2Outside the O, the same quadrat method preparation of this catalyzer with catalyzer U.
Nominal catalyst loading:
2.35 weight %Ru-1.2 weight %Co-5 weight %Re/ high surface area graphitized carbon.
Example 69-catalyzer X
Except with have only 0.15g cobalt salt and ruthenium in soaking step altogether, this catalyzer is with the same quadrat method preparation of catalyst V.
Nominal catalyst loading:
2.35 weight %Ru-0.60 weight %Co-5 weight %Re/ high surface area graphitized carbon.
The X-ray diffraction analysis of alloy catalyst
All sample inspections show unalloyed second kind of metal (iron or cobalt), but does not provide any evidence to the existence of unalloyed ruthenium.All samples, promptly catalyzer U, V, W and X also show the unidentified crystalline material that significant quantity is arranged.Few of available information in the X-ray diffraction studies document of Ru-Fe and Ru-Co alloy.But on atomicity, the content of the ruthenium of these catalyzer always equals second metal at least, and possible unidentified material is a kind of Ru-Fe and Ru-Co alloy of rich rhodium.
Catalyst test
The hydrogenation of acetate
Step
Reaction is to finish in once by the plug flow microreactor with a 2.5ml catalyst charge.Total reaction agent pressure maintains 10barg.LHSV is approximately 1.35, and the ratio of hydrogen and acetate is 10: 1.Reaction product detects the gas chromatograph analysis with flame ionization detection and thermal conduction.
The result is about 230 ℃ three differing tempss, obtains under about 210 ℃ and about 190 ℃.
Comparative experiments 23
Catalyzer T uses as the same step.
The result provides in table 12.
Example 70-73
Catalyzer U, V, W and X use as top step.
The result provides in table 12.
Table 12
T U V W X
Catalyzer
Actual temperature (℃) 234 233 235 230 230
Transformation efficiency (%) 41.32 55.40 56.67 43.46 36.08
Selectivity (CH
4) (%) 33.04 16.89 14.21 18.80 12.85
Selectivity (C
2H
6) (%) 14.19 7.77 7.11 9.18 6.99
Selectivity (EtOH) (%) 47.80 54.83 64.80 62.07 71.90
Selectivity (EtOAc) (%) 4.34 18.03 13.28 8.42 7.45
T U V W X
Catalyzer
Actual temperature (℃) 215 210 215 210 210
Transformation efficiency (%) 26.01 32.05 32.21 27.14 25.26
Selectivity (CH
4) (%) 26.25 11.42 8.03 13.64 9.66
Selectivity (C
2H
6) (%) 11.28 6.25 4.88 7.61 5.63
Select Jian Yu ‥ tOH) (%) 57.25 66.30 68.51 70.65 67.29
Selectivity (EtOAc) (%) 4.81 11.45 18.19 6.40 15.72
T U V W X
Catalyzer
Actual temperature (℃) 194 191 192 195 192
Transformation efficiency (%) 14.45 19.99 13.52 19.41 14.91
Selectivity (CH
4) (%) 18.79 7.80 6.40 10.69 5.61
Selectivity (C
2H
6) (%) 8.96 4.87 4.79 6.39 4.05
Selectivity (EtOH) (%) 66.83 72.02 77.01 40.83 63.85
Selectivity (EtOAc) (%) 4.91 9.67 10.58 40.24 23.74
Errata
Claims (18)
1, a kind of production method that forms corresponding alcohol and/or carboxylicesters by a carboxylic acid or its acid anhydrides, this method comprises the high temperature hydrogenation reaction in the presence of catalyzer of carboxylic acid or its acid anhydrides, catalyzer comprises a kind of alloy, this alloy be the precious metal of (I) at least a periodic table of elements VIII family and (II) at least a can with VIII family precious metal interfused metal.
2, according to the method for claim 1, the precious metal that it is characterized in that VIII family is in palladium, rhodium, the ruthenium.
3, according to the method for claim 1, it is characterized in that precious metal is a palladium, can be in silver, gold and the copper with the metal of the molten gold of precious metal.
4, require according to aforesaid right in each described method, it is characterized in that catalyzer incorporates at least one in rhenium metal, tungsten, the molybdenum into.
5, require according to aforesaid right in each described method, it is characterized in that the composition of catalyzer is attached to the graphitized carbon of a high surface area, graphite, activated carbon, silicon-dioxide is on one in aluminum oxide or the silica/alumina.
6,, it is characterized in that catalyzer comprises (I) palladium and silver-colored alloy and (II) rhenium is attached on the graphitized carbon of a high surface area according to each described method in the aforesaid right requirement.
7, according to each described method in the aforesaid right requirement, it is characterized in that using a kind of carboxylic acid with chemical formula R-COOH, wherein R is C
2-C
12Alkyl, perhaps use its a kind of acid anhydrides.
8, according to the method for claim 7, it is characterized in that using a kind of carboxylic acid, it can be a kind of in acetate, propionic acid, butyric acid or the enanthic acid.
9,, it is characterized in that using a kind of saturated or unsaturated di-carboxylic acid or its a kind of acid anhydrides according to each described method in the claim 1 to 6.
10, according to the method for claim 9, it is characterized in that using a saturated or undersaturated dicarboxylic acid, it is in pentanedioic acid, Pyroglutaric acid, hexanodioic acid, adipic anhydride, succsinic acid, succinyl oxide, toxilic acid or the maleic anhydride one.
11, a kind of method from toxilic acid or maleic anhydride production r-butyrolactone, this method comprises toxilic acid or the high temperature hydrogenation reaction of maleic anhydride in the presence of catalyzer, this catalyst composition comprises a kind of alloy, alloy be at least one precious metal in (I) periodic table of elements VIII family and (II) at least one can with precious metal interfused metal.
12,, it is characterized in that precious metal is in palladium, rhodium, the ruthenium according to the method for claim 11.
13, according to the method for claim 12, it is characterized in that precious metal is a palladium, can be in silver, gold or the copper one with precious metal interfused metal.
14,, it is characterized in that to be silver with palladium interfused metal according to the method for claim 13.
15, according to each described method in the claim 11 to 14, it is characterized in that catalyst composition incorporates a kind of carrier into, this carrier is a kind of in high surface area graphitized carbon, graphite, activated carbon, silicon-dioxide, aluminum oxide or the silica/alumina.
16,, it is characterized in that carrier is the graphitized carbon of high surface area according to the method for claim 15.
17,, it is characterized in that toxilic acid or maleic anhydride introduce as a kind of solution according to each described method in the claim 11 to 16.
18, according to each described method in the aforesaid right requirement, it is characterized in that catalyzer is activated before use.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 90108710 CN1024795C (en) | 1987-03-31 | 1988-03-31 | Catalysed hydrogenation of carboxylic acids and their anhydrides to alcohols and/or esters |
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|---|---|---|---|
| GB8707595 | 1987-03-31 | ||
| GB878707595A GB8707595D0 (en) | 1987-03-31 | 1987-03-31 | Chemical process |
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| CN 90108710 Division CN1024795C (en) | 1987-03-31 | 1988-03-31 | Catalysed hydrogenation of carboxylic acids and their anhydrides to alcohols and/or esters |
| CN91103253A Division CN1027043C (en) | 1987-03-31 | 1988-03-31 | Hydrogenation catalyst for producing alcohols and/or esters from carboxylic acids and their anhydrides |
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| CN1017703B CN1017703B (en) | 1992-08-05 |
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| CN88102591A Expired CN1017703B (en) | 1987-03-31 | 1988-03-31 | Catalysed hydrogenation of carboxylic acids and their anhydrides to alcohols and/or esters |
| CN91103253A Expired - Lifetime CN1027043C (en) | 1987-03-31 | 1988-03-31 | Hydrogenation catalyst for producing alcohols and/or esters from carboxylic acids and their anhydrides |
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|---|---|
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| EP (3) | EP0417867B1 (en) |
| JP (1) | JP2749090B2 (en) |
| CN (2) | CN1017703B (en) |
| AT (2) | ATE63106T1 (en) |
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
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- 1988-03-30 JP JP63502763A patent/JP2749090B2/en not_active Expired - Lifetime
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- 1988-03-30 WO PCT/GB1988/000241 patent/WO1988007515A1/en unknown
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- 1988-03-31 CN CN91103253A patent/CN1027043C/en not_active Expired - Lifetime
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| CN102149662A (en) * | 2008-07-31 | 2011-08-10 | 国际人造丝公司 | Ethanol production from acetic acid utillizing a cobalt catalyst |
| CN102149668A (en) * | 2008-07-31 | 2011-08-10 | 国际人造丝公司 | Direct and selective production of ethyl acetate from acetic acid utilizing a bimetal supported catalyst |
| CN102311311B (en) * | 2008-07-31 | 2015-07-15 | 国际人造丝公司 | Direct and selective production of ethanol from acetic acid utilizing a platinum/tin catalyst |
| US8487143B2 (en) | 2008-07-31 | 2013-07-16 | Celanese International Corporation | Ethanol production from acetic acid utilizing a cobalt catalyst |
| CN102272089A (en) * | 2008-12-31 | 2011-12-07 | 国际人造丝公司 | Integrated process for the production of vinyl acetate from acetic acid via ethyl acetate |
| CN102272089B (en) * | 2008-12-31 | 2014-08-20 | 国际人造丝公司 | Integrated process for the production of vinyl acetate from acetic acid via ethyl acetate |
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| CN102688758A (en) * | 2011-03-22 | 2012-09-26 | 中国科学院大连化学物理研究所 | Catalyst for preparing ethanol by acetic acid gas phase hydrogenation and preparation method thereof |
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| CN103861635A (en) * | 2012-12-13 | 2014-06-18 | 洛阳市科创石化科技开发有限公司 | Catalyst for ethanol preparation through direct hydrogenation of acetic acid, preparation method and application thereof |
| CN105646152A (en) * | 2014-12-04 | 2016-06-08 | 中国石油化工股份有限公司 | Preparation method of 1, 2-benzenedimethanol |
| CN111606804A (en) * | 2019-02-26 | 2020-09-01 | 中国石油化工股份有限公司 | Method for preparing adipate derivatives |
| CN113968783A (en) * | 2020-07-22 | 2022-01-25 | 中国石油化工股份有限公司 | Method for preparing short-carbon-chain dicarboxylic acid ester derivative |
| CN113968783B (en) * | 2020-07-22 | 2023-10-10 | 中国石油化工股份有限公司 | Method for preparing short carbon chain dicarboxylic ester derivative |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2749090B2 (en) | 1998-05-13 |
| CN1059296A (en) | 1992-03-11 |
| EP0417867B1 (en) | 1995-09-27 |
| EP0662343A1 (en) | 1995-07-12 |
| AU602208B2 (en) | 1990-10-04 |
| DE3854529D1 (en) | 1995-11-02 |
| NZ224073A (en) | 1990-08-28 |
| DE3854529T2 (en) | 1996-03-28 |
| ATE128381T1 (en) | 1995-10-15 |
| EP0285420A1 (en) | 1988-10-05 |
| DE3862601D1 (en) | 1991-06-06 |
| CN1017703B (en) | 1992-08-05 |
| EP0285420B1 (en) | 1991-05-02 |
| US4985572A (en) | 1991-01-15 |
| AU1497888A (en) | 1988-11-02 |
| EP0417867A1 (en) | 1991-03-20 |
| GB8707595D0 (en) | 1987-05-07 |
| ATE63106T1 (en) | 1991-05-15 |
| JPH01503459A (en) | 1989-11-22 |
| WO1988007515A1 (en) | 1988-10-06 |
| CN1027043C (en) | 1994-12-21 |
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